Combustion with variable oxidant low nox burner

ABSTRACT

Heating provided by a burner that combusts hydrocarbon fuel can be provided at a sequence of different heat transfer rates by adjusting the total oxygen concentration of oxidant streams fed to the burner. A burner with which the method can be practiced is also disclosed.

This application claims priority from U.S. provisional application Ser.No. 60/872,725 filed Dec. 4, 2006, the content of which is herebyincorporated herein by reference.

FIELD OF THE INVENTION

The present invention relates to combustion that generates heat usefulfor heating materials to high temperatures and for holding them at hightemperatures.

BACKGROUND OF THE INVENTION

Many industrial applications require heating materials to hightemperatures for melting, heat treating, and the like. Heat is oftenprovided by combusting hydrocarbon fuels. However, in these applicationsthe need can arise for supplying heat at different heating rates atdifferent times. Conventional approaches to this need can involveheating the material to a desired high temperature, then discontinuingthe combustion in order to let the temperature of the material decrease,and then recommencing combustion when the temperature drops enough thatadditional heat must be applied. Such “on/off” operation is inefficientin its consumption of fuel and oxidant, and it risks generatingunacceptable levels of undesirable byproducts such as nitrogen oxides.Also, it risks imposing thermal stresses on the material by the cyclingof the temperature and/or operational stresses on the valves and burnersthat are repeatedly forced to open and close as the combustion isstopped and started. Other approaches, such as providing two separateburner systems each adapted for a particular type of combustion, withonly one system operated at a time, are expensive and take up space.

Therefore, there remains a need for methods and apparatus that enablemore efficient and more environmentally tolerable heating of materials,especially under conditions in which the amount of heating is to varyover time.

BRIEF SUMMARY OF THE INVENTION

One aspect of the present invention is a burner system comprising aburner body and a burner block, wherein

-   -   (A) the burner body comprises    -   a plenum body which has back and side surfaces that enclose a        plenum space which is open at its front in a uniplanar plenum        opening that is defined by the front edges of said side surface,    -   a feed inlet in a back or side surface of said plenum body,        through which gas can be fed into said plenum space,    -   a first hollow body that is situated completely within said        plenum space and that is closed against passage of gas between        said plenum space and the interior of said hollow body, wherein        the hollow body does not extend through said plenum opening,    -   a feed inlet through a surface of said hollow body, through        which gas can be fed into the interior of said hollow body,    -   2 to 16 outlet ports through a surface of said hollow body,        through which gas can pass out of said hollow body, each        oriented to point outwardly of said plenum space toward the        plenum opening, wherein the outer ends of said outlet ports do        not extend beyond the plane of said plenum opening,    -   a first tube extending from outside the back surface of said        plenum body through the plenum space to a first tube end that is        located a first distance outside the plane of the plenum        opening, wherein the first tube is closed against passage of gas        into said first tube from the plenum space and from the interior        of the hollow body,    -   a second tube, located inside the first tube, extending from        outside the back surface of said plenum body through the plenum        space to a second tube end that is located a second distance        outside the plane of the plenum opening, wherein said second        distance is greater than first distance, wherein said second        tube is closed against passage of gas into said second tube from        the plenum space, from the interior of the hollow body, and from        the first tube, and wherein the axes of the first and second        tubes are coaxial or parallel,    -   a third tube, located inside the second tube, extending from        outside the back surface of said plenum body through the plenum        space to a third tube end that is located said second distance        outside the plane of the plenum opening, wherein said third tube        is closed against passage of gas into said third tube from the        plenum space, from the interior of the hollow body, and from the        second tube, and wherein the axes of the first, second and third        tubes are coaxial or parallel,    -   a feed inlet for receiving gas into the space between the first        and second tubes,    -   a feed inlet for receiving gas into the space between the second        and third tubes, and a feed inlet for receiving fuel into said        third tube; and    -   (B) the burner block comprises    -   a front surface and a rear surface,    -   a first passageway extending through the block, composed of a        barrel segment that extends into the block from said rear        surface to the inner end of said barrel segment for a length at        least equal to said first distance, the diameter of said barrel        segment permitting said first tube to fit snugly into said        barrel segment to minimize passage of gas in said barrel segment        outside said first tube,    -   a throat segment having upstream and downstream ends and whose        diameter is constant along its axis and is less than the        diameter of said barrel segment and is greater than the outer        diameter of said second tube, wherein the distance from the rear        surface of the block to said upstream end is greater than said        first distance and less than said second distance, and wherein        the distance from the rear surface of said block to said        downstream end is greater than said second distance,    -   a tapered segment that extends axially from the inner end of        said barrel segment to said upstream end of said throat segment,    -   a port segment that extends into the block from the front        surface of the block to the inner end of the port segment,        wherein the diameter of the port segment is constant and is        greater than the diameter of said throat segment    -   a quarl segment that extends from the downstream end of said        throat segment to the inner end of said port segment,    -   wherein said segments are coaxial, and the sum of the axial        lengths of the port segment and the quarl segment is up to 50        times the diameter of the largest diameter of the quarl segment;        the axial length of the throat segment is up to 50 times the        diameter of the largest diameter of the quarl segment; the ratio        of the largest diameter of the quarl segment to the diameter of        the throat segment is 1 to 50; and the distance from the        discharge openings of the secondary passageways to the axis of        the first passageway is 1-10 times the diameter of the throat        segment,    -   a plurality of secondary passageways, greater in number than the        number of said outlet ports, extending through said block from        inlet openings in the rear surface of said block to discharge        openings in the front surface of said block, wherein said inlet        openings are close enough to said first passageway that when the        front edges of said plenum body are in contact with the rear        surface of said block, said inlet openings are in gas contact        with said plenum space, and wherein each secondary passageway        has an axis at its discharge opening that converges toward the        axis of the first passageway at an angle of up to 60°, diverges        from the axis of the first passageway at an angle of up to 85°,        or is parallel to the axis of the first passageway;    -   wherein said burner body is positioned with respect to said        burner block so that the front edges of said plenum body are in        contact with the rear surface of said block to prevent passage        of gas out of said plenum space except into said secondary        passageways and the first and second tubes extend into said        first passageway, and outlet ports are aligned with secondary        passageways so that gas passing from an outlet port passes        through a secondary passageway with which it is aligned.

Another aspect of the invention is a method for heating a substrate,comprising

(A) providing the aforementioned burner system,

(B) determining a first rate of heat transfer to the substrate,

(C) determining the rates at which fuel and oxidant are to be fed tosaid burner system to be combusted thereat, and the total oxygenconcentration of said oxidant to be combusted, to generate heat ofcombustion to be transferred to said substrate from said burner systemat said first rate,

(D) feeding fuel, and oxidant having said total oxygen concentration, atsaid rates to said burner system and combusting said fuel and saidoxidant at said system to generate heat of combustion which istransferred to said substrate at said first rate,

while apportioning the amounts of oxygen fed through said first andsecond tubes of said burner system with respect to the amounts of oxygenfed through said secondary passageways and said outlet ports of saidburner system to minimize formation of NOx by said combustion,

(E) determining a second rate of heat transfer to the substrate which isdifferent from said first rate,

(F) determining a new total oxygen concentration of said oxidant to becombusted and determining new rates at which said oxidant, or saidoxidant and said fuel, are to be fed to said burner system and combustedthereat to generate heat of combustion to be transferred to saidsubstrate at said second rate, and

(G) while continuing to feed fuel and oxidant to said burner system,changing the total oxygen concentration fed to said burner system tosaid new total oxygen concentration and changing the rate at which saidoxidant or said oxidant and said fuel are fed to said burner system, andcontinuing to combust said fuel and oxidant at said burner system,without discontinuing said combustion, to generate heat of combustionwhich is transferred to said substrate at said second rate,

while apportioning the amounts of oxygen fed through said first andsecond tubes with respect to the amounts of oxygen fed through saidsecondary passageways and said outlet ports to minimize formation of NOxby said combustion,

wherein the amount of oxygen fed to said burner system is at all timessufficient to maintain combustion of said fuel at said burner system,and wherein the amount of oxygen fed to said burner system is at alltimes sufficient to maintain the carbon monoxide content of the gaseousproducts of said combustion at less than 100 ppm.

As used herein, “NOx” means gaseous oxides of nitrogen, regardless ofthe number of atoms of nitrogen and of oxygen in any individual moleculeof nitrogen and oxide, and mixtures thereof.

As used herein, “total oxygen concentration” means the total amount ofoxygen fed through all inlets of a burner system through which gaseousoxidant is fed, including oxygen in any transport medium that is fedwith fuel, divided by the total amount of gas fed through all inlets ofa burner system through which gaseous oxidant is fed, including gas inany transport medium that is fed with fuel.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a cross-sectional view of a burner block that can be acomponent of the burner system with which the present invention can beutilized.

FIG. 2 is a perspective view of the front surface of a burner block withwhich the present invention can be utilized.

FIG. 3 is a perspective view of a burner body which can be a componentof a burner system with which the present invention can be utilized.

FIG. 4 is a cross-sectional view of a burner body and burner blockassembled together to form a burner system with which the presentinvention can be used.

DETAILED DESCRIPTION OF THE INVENTION

The present invention is useful in any situation requiring heat transferat a sequence of two or more different rates to a substrate, where thesubstrate or material in contact with the substrate is heated totemperatures (typically above 1000F) on the order of the temperaturesthat can be attained by combustion of hydrocarbon fuels such as naturalgas, fuel oil, and the like. Suitable “substrates” with which thisinvention can be utilized include any material that one desires to heat,including in particular solids and liquids, such as metals and metallicprecursors, whether to melt the solids, to melt solids already containedin liquid baths, to maintain a solid or a molten liquid at a desiredhigh temperature, or to heat or preheat a container such as a ladlewhich is to receive and hold hot material.

One example of a use for this invention is in melting material byapplying heat at a relatively high rate, then holding the resultingmolten material at high temperature by applying heat at a lower heattransfer rate. Another example is preheating a ladle or tundish intowhich hot solid or molten material is to be fed, in which the ladle ortundish is heated at a high rate to a temperature at or near thetemperature of the material, and then holding the hot solid or moltenmaterial at high temperature after it has been fed to the ladle ortundish, by applying heat at a relatively lower rate.

The present invention can be practiced usefully with burner systems suchas the burner system illustrated in FIGS. 1-4 and described below. Suchburner systems typically include a burner block, and a burner bodyassembled with the burner block to form the burner system.

Referring first to FIG. 1, burner block 1 is shown before it isassembled with the burner body. Burner block 1 is a solid body ofmaterial capable of withstanding the elevated temperatures to which itis necessarily subjected when combustion is carried out at the burnerbody. Suitable materials of construction include refractory brick, suchas high alumina, alumina, silica, AZS, mulite, zirconia, and/orzirconite, as well as metal structure including water-cooled metalstructures.

Burner block 1 includes front surface 2 and rear surface 3. Firstpassageway 4 passes through burner block 1 from rear surface 3 to frontsurface 2. First passageway 4 is comprised of a series of coaxialsegments, each contributing to the performance of the burner system whenthe burner body is assembled together with the burner block.

Proceeding from the rear surface 3 of burner block 1, barrel segment 5extends into burner block 1 from the rear surface, preferably as acylinder of constant diameter if the section of burner body that willextend into barrel segment 5 is also cylindrical. The cross-sectionalconfiguration of barrel segment 5 is preferably dimensioned to providedfor a snug fit with the section of the burner body that is to occupybarrel segment 5, as described below. Preferably, the fit is snug enoughthat passage of gasses between the inner surface of barrel segment 5 andthe outer surface of the corresponding section of the burner body isminimized or even prevented. The length of barrel segment 5, that is,its depth measured into burner block 1 from the rear surface 3 of burnerblock 1, is at least as long as the length of first tube 41 of burnerbody described herein.

Proceeding further into first passageway 4, tapered segment 6 extendsfrom the inner end of barrel segment 5 to the upstream end of throatsegment 7. The surface of tapered segment 6 can be flat (so that it is asection of a cone) or can be curved (i.e. so that the radius changes ata nonconstant rate along the axis).

Throat segment 7 is preferably of constant diameter, and is narrowerthan barrel segment 5. Thus, tapered segment 6 necessarily has a smallercross-sectional area and diameter at its downstream end where itintersects throat segment 7 than at its upstream end where it intersectswith barrel segment 5. Throat segment 7 is situated within burner block1 so that its upstream end is closer to the rear surface of burner block1 than is the end of second tube 43, as described further below. Thedownstream end of throat segment 7 should be further from the rearsurface of burner block 1 than the end of second tube 43 is. In thatway, the end of second tube 43 is situated within throat segment 7.

Throat segment 7 is connected at its downstream end to the upstream endof quarl segment 8, which is of increasing diameter with increasingaxial distance from the rear surface of burner block 1. Quarl segment 8ends at its downstream end at port segment 9, which is a segment ofconstant diameter larger than the diameter of throat segment 7. Thesurface of quarl segment 8 can be flat (so that it is a section of acone) or can be curved (i.e. so that the radius changes at a nonconstantrate along the axis). Port segment 9 ends where it opens at the frontsurface 2 of burner block 1.

Burner block 1 also has a plurality of secondary passageways 11, each ofwhich passes through burner block 1 from its rear surface to its frontsurface. Each secondary passageway 11 has an inlet opening 12 in therear surface of burner block 1, and a discharge opening 13 in the frontsurface of burner block 1. From 2 to 16, and preferably 4 to 12,secondary passageways 11 extend through burner block 1. There should bemore secondary passageways 11 through burner block 1 than the number ofoutlet ports 33 on the burner body with which the burner block isassembled.

The axis of each secondary passageway 11 can be parallel to the axis offirst passageway 4, but preferably the axis of each secondary passageway11 diverges or may converge with respect to the axis of passageway 4. Asillustrated in FIG. 1, the respective axes diverge from the axis offirst passageway 4; the preferred angle of the divergence is up to 85degrees, more preferably up to 75 degrees. However, if desired, the axesof the secondary passageways can converge, toward the axis of firstpassageway 4, in which case the preferred angle of convergence is up to60 degrees, more preferably up to 15 degrees.

Certain dimensional relationships between different portions of theburner block assist in carrying out the present invention. Thus, the sumof the axial lengths of the port segment and the quarl segment is up to50 times the largest diameter of the quarl segment, and preferably up to25 times that largest diameter. The axial length of the throat segmentis up to 50 times, and more preferably up to 25 times, the diameter ofthe largest diameter of the quarl segment. The ratio of the largestdiameter of the quarl segment to the diameter of the throat segment is 1to 50, and preferably 1 to 25. The distance from the discharge openings13 of the secondary passageways 11 to the axis of the first passageway 4is 1 to 10, and preferably 1.5 to 8, times the diameter of the throatsegment.

FIG. 2 illustrates an embodiment of the front of burner block 1. Thedischarge openings 13 of secondary passageways 11 can be seen, as canport segment 9, quarl segment 8, and the downstream end of throatsegment 7. The burner body illustrated in FIG. 3 would be appropriatefor assembly together with the burner block illustrated in FIG. 2,because the burner body of FIG. 3 contains only two outlet ports 33 eachof which would be aligned with one of the secondary passageways 11,leaving additional secondary passageways 11 through which gas can flowfrom plenum space 23 out the respective discharge openings 13.

FIG. 3 illustrates a burner body useful in the practice of thisinvention. Burner body 21 includes plenum housing 22 formed by plenumback 24 and plenum sides 25 which are sealed together to enclose plenumspace 23. If the plenum cross-section is rectangular, then plenum sides25 may comprise planar surfaces forming a top, two sides, and a bottom.Preferably, the plenum cross-section is round and more preferablycircular, in which case plenum sides 25 are in one continuous surface.In any case, plenum sides 25 terminate in front edge or edges 26 whichform a uniplanar opening, that is, they define a plenum opening throughwhich gas can flow as described herein. Flange 28 is preferably providedto provide a better seal with rear surface 3 of burner block 1. Inlet 27communicates with plenum space 23, and can be connected to a source orsources of the gas to be supplied into plenum space 23 as describedherein.

Burner body 21 also includes hollow body 31 which is situated completelywithin the plenum space 23.

Hollow body 31 completely encloses a space, which can be fed gas by wayof feed inlet 32. Outlet ports 33 permit gas to flow out of the interiorof hollow body 31. From 1 to 16, and preferably 1 to 4, outlet ports 33are provided. Each outlet port 33 terminates at an end 34 which canextend up to, but not through or out of, the plane formed by front edges26 of plenum housing 22. In that way, when the burner body is assembledto burner block 1, such that the front edges 26 contact the rear surface3 of burner block 1 and seal the junction between those two pieces ofapparatus, the outlet ports 33 do not extend out so far that suchcontact is impeded.

At least part, and preferably all, of the front surface 35 of hollowbody 31 is spaced from the plane formed by front edges 26, so thatplenum space 23 is considered to include not only space between theouter surfaces of hollow body 31 and the inner surfaces of plenumhousing 22, but also space between front surface 35 and the plane formedby front edges 26. That spacing permits gas to flow from plenum space 23to the openings 12 of passageways 11 that are not aligned by outletports 33.

Burner body 21 also includes first tube 41, which ends at first tube end42. First tube 41 passes completely through plenum space 23 andprotrudes beyond the plane formed by front edges 26. First tube 41either passes through hollow body 31 as well, or is located next tohollow body 31 within plenum space 23.

Second tube 43 is located inside first tube 41, and third tube 45 islocated within second tube 43. Second tube 43 and third tube 45terminate at second tube end 44 and third tube end 46, respectively,both of which are located further from the plane formed by front edges26 than the first tube end 42. That is, second tube 43 and third tube 45both extend away from plenum housing 22 further than first tube 41extends. Second tube end 44 and third tube end 46 are preferablycoplanar.

The openings at the respective tube ends 42, 44 and/or 46 can becompletely unobstructed, or any of them can contain segments that breakthe openings up into sub-openings which divide the emerging streams intosub-streams. For instance, a plate with a number of holes can be placedacross the opening at the end 46 of third tube 45 to divide the fuelinto a spray of a number of sub-streams.

Vanes can optionally be placed within space 47 and/or space 48 (withinwhich gaseous oxidant streams can flow) to impart swirl that helpsmaintain flammability of the flame at the end of the burner.

The innermost tube, namely third tube 45, preferably receives the fuelwhich is to be combusted as described herein. Suitable fuels can begaseous, liquid, solid, or any combination thereof, such as natural gas,LPG, propane, butane, fuel oil, diesel oil, coke oven gas, blast furnacegas, BOF gas, electric arc furnace gas, producer gas, any type of solidfuel, including slurries with some heating value. For operation withliquid fuel, an atomizing fluid (such as air, oxygen, nitrogen, fuelgas, argon, and steam) could be used. A nozzle to promote atomization ofliquid fuel (with any kind of atomizing media, such as air, steam orother types of gas, or pressure atomizer) may be helpful. For operationwith solid fuel, pulverizing it and then conveying it suspended in acarrier gas (such as air, nitrogen, argon, steam, fuel gas) would behelpful.

Referring to FIG. 4, the cooperation between burner block 1 and burnerbody 21 can be seen. With the front edges 26 of plenum housing 22 fullyin contact with the rear surface 3 of burner block 1, gas cannot passaround those front edges 26. With burner body 21 so positioned againstburner block 1, first tube 41 extends into barrel segment 5 which, asdescribed above, is of a depth at least sufficient to receive the entirelength of first tube 41. Second tube 43 and third tube 45 extend beyondthe end 42 of first tube 41, into throat segment 7 but not past thedownstream end of throat segment 7. In addition, the inlet openings 12of secondary passageways 11 are close enough to first passageway 4 thatthey communicate directly with plenum space 23, so that gas can flowdirectly from plenum space 23 into and through secondary passageways 11and out the respective discharge openings 13. FIG. 4 illustrates twooutlet ports 33 aligned for flow of gas out of their respective endsinto two passageways 11. However, as stated, gas also flows from plenumspace 23 into other passageways 11, not shown in this particularcross-section, that are not aligned with outlet ports 33.

The upstream end of third (fuel) tube 45 is connected to a source offuel through apparatus well known in this field which can feed fuel inany amount and rate desired, and can vary the amount and rate offeeding, and can turn on and shut off the flow of fuel when desired.Fuel is preferably fed at a rate of 10 to 1500, more preferably 15 to1000, m/sec, and at a temperature of up to 1800° C.

The upstream end of space 47 between tubes 41 and 43, the upstream endof space 48 between tubes 43 and 45, as well as inlet 27 to plenum space23, and inlet 32 to hollow body 31, are each connected by appropriatefeed lines, valves, and controls to sources of gaseous oxidant (ormixtures of oxygen and one or more non-oxygen gases), thereby to permitcontrol of the oxygen content of each of those gaseous streams, as wellas the flow rates of each of those gaseous streams. In addition tocontrols that permit the flow of gas to any of these points to be turnedon and shut off, controls that enable the practice of the presentinvention must also be present that enable the oxygen content and theflow rate of each such gaseous stream to be adjusted to any desiredvalue as described herein, even while combustion is ongoing at theburner.

The upstream end of space 47 that feeds “primary oxidant” should beconnected to gas sources and controls that enable the gaseous stream fedto space 47 to have (a) an oxygen content as low as the lowest that itmay be desirable to feed into space 47, preferably at least 5 vol. % andmore preferably at least 10 vol. %, (b) an oxygen content as high as thehighest concentration that it may be desirable to feed into space 47,preferably at least 90 vol. % and more preferably at least 99.9 vol. %,and (c) an oxygen concentration anywhere between those lowest andhighest values. This can be achieved by providing a source of highpurity oxygen (at a purity that equals the highest concentration that isto be available for feeding into space 47), and providing a source ofgas having the indicated lowest desired oxygen concentration, as well asoptionally a source of gas (such as air) having an oxygen concentrationbetween those lowest and highest values.

Controls should also be provided for controlling the amount of gas fedfrom each such gas source, so that any desired intermediate oxygenconcentration that is between those lowest and highest values can becomposed. A stream having any such intermediate oxygen concentration canbe provided by combining streams from the respective sources upstreamfrom space 47 and then feeding the combined stream into space 47, or byfeeding streams from each source into the upstream end of space 47 inthe appropriate relative amounts so that they mix in space 47 and form amixture having the desired intermediate oxygen concentration. Theoxidant should be supplied at a rate so that the stream emerges from end42 of tube 41 at a velocity of 10 to 1500, preferably 15 to 500, m/sec.The temperature of the stream as it emerges is up to 1800° C.

Inlet 27 that feeds “secondary oxidant” via plenum 21 should beconnected to gas sources and controls that enable the gaseous stream fedto inlet 27 to have (a) an oxygen content as low as the lowest that itmay be desirable to feed into inlet 27, preferably at least 5 vol. % andmore preferably at least 10 vol. %, (b) an oxygen content as high as thehighest concentration that it may be desirable to feed into inlet 27,preferably at least 90 vol. % and more preferably at least 99.9 vol. %,and (c) an oxygen concentration anywhere between those lowest andhighest values. This can be achieved by providing a source of highpurity oxygen (at a purity that equals the highest concentration that isto be available for feeding into inlet 27), and providing a source ofgas having the indicated lowest desired oxygen concentration, as well asoptionally a source of gas (such as air) having an oxygen concentrationbetween those lowest and highest values.

Controls should also be provided for controlling the amount of gas fedfrom each such gas source, so that any desired intermediate oxygenconcentration that is between those lowest and highest values can becomposed. A stream having any such intermediate oxygen concentration canbe provided by combining streams from the respective sources upstreamfrom inlet 27 and then feeding the combined stream into inlet 27, or byfeeding streams from each source into the upstream end of inlet 27 inthe appropriate relative amounts so that they mix in inlet 27 and form amixture having the desired intermediate oxygen concentration. Theoxidant should be supplied at a rate so that the stream emerges fromdischarge openings 13 at a velocity of 5 to 1500, preferably 6 to 1200,m/sec. The temperature of the stream as it emerges is up to 1800° C.

The upstream end of space 48 that feeds “primary oxygen” should beconnected to gas sources and controls that enable the gaseous stream fedto space 48 to have (a) an oxygen content as low as the lowest that itmay be desirable to feed into space 48, which may be zero (that is, thesource provides a gas or a mixture of gases none of which is oxygen) andpreferably at least 50 vol. %, (b) an oxygen content as high as thehighest concentration that it may be desirable to feed into space 48,preferably at least 90 vol. % and more preferably at least 99.9 vol. %,and (c) an oxygen concentration anywhere between those lowest andhighest values. This can be achieved by providing a source of highpurity oxygen (at a purity that equals the highest concentration that isto be available for feeding into space 48), and providing a source ofgas having the indicated lowest desired oxygen concentration, as well asoptionally a source of gas (such as air) having an oxygen concentrationbetween those lowest and highest values.

Controls should also be provided for controlling the amount of gas fedfrom each such gas source, so that any desired intermediate oxygenconcentration that is between those lowest and highest values can becomposed. A stream having any such intermediate oxygen concentration canbe provided by combining streams from the respective sources upstreamfrom space 48 and then feeding the combined stream into space 48, or byfeeding streams from each source into the upstream end of space 48 inthe appropriate relative amounts so that they mix in space 48 and form amixture having the desired intermediate oxygen concentration. Theoxidant should be supplied at a rate so that the stream emerges from end44 of tube 43 at a velocity of 10 to 1500, preferably 15 to 500, m/sec.The temperature of the stream as it emerges is up to 1800° C.

Inlet 32 that feeds “secondary oxygen” via hollow body 31 and outletport(s) 33 should be connected to gas sources and controls that enablethe gaseous stream fed to inlet 32 to have (a) an oxygen content as lowas the lowest that it may be desirable to feed into inlet 32, which maybe zero (that is, the source provides a gas or a mixture of gases noneof which is oxygen) and preferably at least 50 vol. %, (b) an oxygencontent as high as the highest concentration that it may be desirable tofeed into inlet 32, preferably at least 90 vol. % and more preferably atleast 99.9 vol. %, and (c) an oxygen concentration anywhere betweenthose lowest and highest values. This can be achieved by providing asource of high purity oxygen (at a purity that equals the highestconcentration that is to be available for feeding into inlet 32), andproviding a source of gas having the indicated lowest desired oxygenconcentration, as well as optionally a source of gas (such as air)having an oxygen concentration between those lowest and highest values.

Controls should also be provided for controlling the amount of gas fedfrom each such gas source, so that any desired intermediate oxygenconcentration that is between those lowest and highest values can becomposed. A stream having any such intermediate oxygen concentration canbe provided by combining streams from the respective sources upstreamfrom inlet 32 and then feeding the combined stream into inlet 32, or byfeeding streams from each source into the upstream end of inlet 32 inthe appropriate relative amounts so that they mix in inlet 32 and form amixture having the desired intermediate oxygen concentration. Theoxidant should be supplied at a rate so that the stream emerges fromdischarge openings 13 at a velocity of 5 to 1500, preferably 6 to 1200,m/sec. The temperature of the stream as it emerges is up to 1800° C.

Of course, the same source of a given gas (such as a cylinder or airseparation unit that provides high purity oxygen) can be used inproviding a gas stream to more than one of the aforementioned inputs.

Using the Burner System

Now the use of the burner system will be described.

In the first phase of the method of the present invention, the heatingneeds are determined. The amount of heat to be transferred to thesubstrate is determined, on the basis of such factors as a desiredincrease in the temperature of the substrate, the mass of the substrate,the heat capacity, the heat of fusion if melting is to occur, and thelike. The period of time within which the heat transfer is to beachieved is determined, giving the desired first rate of heat transferto the substrate.

The temperature of the flame produced at the burner, to impart the heattransfer that is required for this first phase of the operation, can beachieved by setting the total oxygen concentration in the oxidantstreams that are fed and combusted for a given degree of recirculationof the flue gas. At any given flue gas recirculation ratio, the flametemperature increases with increasing total oxygen concentration. At anygiven total oxygen concentration, the flame temperature increases withdecreasing flue gas recirculation ratio. This permits determination ofan effective total oxygen concentration in the oxidant streams fedthrough the burner, to achieve the required temperature.

Fuel is then combusted in a burner system such as that described herein,with oxygen that is fed as gaseous oxidant streams through and out ofspaces 48 and/or 50, and that is fed out of discharge openings 13 ofsecondary passageways 11, having entered those secondary passagewaysfrom outlet ports 33 and/or from plenum space 23. The total amount ofoxygen fed should be 0.6 to 2.0 times the amount of oxygen needed forcomplete combustion of the fuel. The fuel combusts in a flame whose baseis at the end 46 of third (fuel) tube 45. The amount of oxygen fed tothe burner system must be sufficient to enable combustion of the fuel tobe maintained, at must be sufficient to provide that the fuel issufficiently combusted so that the carbon monoxide content of thegaseous combustion products (i.e. the flue gas) produced by thecombustion is less than 100 ppm. Also, as described more fully below,the feeds of gaseous oxidant are adjusted so that the amount of NOxformed by the combustion is minimized.

Then, in the second phase of the method of the present invention, whenthe heat transfer rate to the substrate is to change, the new (second)heat transfer rate is determined, again by considerations of factorssuch as a desired change (increase or decrease) in the temperature ofthe substrate, the mass of the substrate, the heat capacity, the heat offusion if melting or solidification is to occur, and the like. Theperiod of time within which the heat transfer is to be achieved isdetermined, giving the desired second rate of heat transfer to thesubstrate.

The temperature of the flame produced at the burner, to impart thedesired second rate of heat transfer that is required for this secondphase of the operation, can be achieved by setting the total oxygenconcentration in the oxidant streams that are fed and combusted for agiven degree of recirculation of the flue gas. At any given flue gasrecirculation ratio, the flame temperature increases with increasingtotal oxygen concentration. At any given total oxygen concentration, theflame temperature increases with decreasing flue gas recirculationratio. This permits determination of an effective total oxygenconcentration in the oxidant streams fed through the burner, to achievethe required temperature.

Fuel is then combusted in a burner system such as that described herein,with oxygen that is fed as gaseous oxidant streams through and out ofspaces 48 and/or 50, and out discharge openings 13 of secondarypassageways 11, having entered those secondary passageways from outletports 33 and/or from plenum space 23. The total amount of oxygen fedshould be 0.6 to 2.0 times the amount of oxygen needed for completecombustion of the fuel. The amount of oxygen fed to the burner systemmust be sufficient to enable combustion of the fuel to be maintained, atmust be sufficient to provide that the fuel is sufficiently combusted sothat the carbon monoxide content of the gaseous combustion products(i.e. the flue gas) produced by the combustion is less than 100 ppm.Also, as described more fully below, the feeds of gaseous oxidant areadjusted so that the amount of NOx formed by the combustion isminimized.

The preferred modes of carrying out combustion, and especially ofmodifying the combustion conditions (especially the total oxygenconcentration) with various total oxygen concentrations, are as follows.

For combustion with a total oxygen concentration lower than 21% byvolume, a portion of the total oxygen for combustion is introduced asprimary oxidant through space 48, and the remaining oxygen required tocomplete the combustion process is introduced into plenum space 23 fromwhich it passes through the secondary passages 11 and out of thedischarge openings 13. This arrangement stages the combustion in a waythat lowers the flame peak temperature, and consequently the NOxemission rate is lowered.

For combustion with total oxygen concentrations greater than or equal to21 vol. % and less than 28 vol. %, one of the following procedures ispreferred:

One preferred procedure is feeding oxidant through both of spaces 48 and50, and raising the oxygen concentration of the oxidant steam fed intospace 50 by adding oxygen (preferably as a stream of at least 90 vol. %purity oxygen) to that oxidant before feeding the resulting mixture intospace 50. If desired, the amount of oxidant fed through space 48 isreduced or eliminated. The remaining oxygen required to complete thecombustion process is supplied in the oxidant that is fed into plenuminlet 27 and into inlet 32 for hollow body 31, from where it enterssecondary passageways 11 and flows out of discharge openings 13. Due tothe elimination or significant reduction of the nitrogen content thatresults from the addition of the high purity oxygen, combined with thestaging effect provided by the oxygen that is fed from the secondarypassageways 11, the NOx emission rate is reduced.

A second preferred procedure with total oxygen concentrations greaterthan or equal to 21 vol. % and less than 28 vol. %, is feeding oxidantinto and through space 48, without feeding any oxidant through space 50,and feeding the remaining oxygen required to complete the combustionprocess through the secondary passageways 11 from plenum space 23 andfrom hollow body 31. Due to the lower oxygen concentration in the fuelstream and in the stream emerging from space 48 compared to the firstembodiment above, the temperature of the base of the flame tends to belower. Due to this fact, the NOx emission rate is expected to be lower.

For combustion with total oxygen concentrations greater than or equal to28 vol. %, one of the following operating procedures is preferred:

(a) One preferred procedure is feeding oxygen through space 50, withoutfeeding any oxidant through space 48, and feeding the remaining oxygenrequired to complete the combustion into plenum space 23 and into hollowbody 31 so that it passes through the secondary passageways 11 andcombusts. The amount of oxygen in the oxidant introduced through theplenum is gradually reduced while the amount of oxygen in the oxidantintroduced through the hollow body 31 and outlet ports 33 is graduallyincreased. The total oxygen introduced through the secondary passagewaysis determined based on the combustion process requirements. Due to theabsence of nitrogen, or at least the significant reduction in the amountof nitrogen introduced with the oxygen, combined with the staging effectpromoted by the oxidant streams fed out of the secondary passageways,the NOx emission rate is reduced.

(b) A second preferred procedure is feeding oxygen into and throughspace 48, and feeding the remaining oxygen required to complete thecombustion into plenum space 23 and hollow body 31 so that it passesthrough and out of the secondary passageways 11. The amount of oxygenintroduced through plenum 23 is gradually reduced while the amount ofoxygen introduced through hollow body 31 increases. The total amount ofoxygen introduced through the secondary passageways is determined basedon the combustion process requirements. Due to the elimination orsignificant reduction of nitrogen in the oxidant feed streams, combinedwith the staging effect promoted by feeding oxygen from the secondarypassageways, the NOx emission rate is reduced.

(c) A third procedure is feeding oxidant or high purity (at least 90vol. % oxygen) through only inlets 50 and 32, without feeding anyoxidant through inlets 48 and 27. Due to the elimination of the otheroxidant streams, combined with the staging effect provided by thestreams emerging from secondary passageways that are fed from outletports 33, the NOx emission rate is reduced to the lowest level.

NOx Control

In each phase of the method of the present invention, the flows ofgaseous oxidant to the respective outlets of the burner system areadjusted so that NOx production is minimized. The burner design of theinvention disclosed herein enables establishing low minimized NOxemission levels at any of the various combustion conditions. To minimizeNOx production during combustion, one or more of the following methodscan be employed:

staging of the oxygen contents between the oxidant streams that are fedfrom spaces 48 and 50, and the oxidant streams that are fed from thesecondary passageways;

feeding oxygen of at least 90 vol. % to spaces 48 and/or 50 (therebyminimizing the nitrogen content in those streams) only when operatingthe burner with total oxygen concentration above 20.9 vol. %;

the secondary passageways 11 all forming diverging angles relative tothe axis of the first passageway 4.

The staging, and the degree of staging, can be accomplished by varyingany one or more of the following parameters:

The ratio between the flow rates and the oxygen contents of the streamemerging from space 48 and the streams fed by the plenum,

The ratio of the oxygen flow rates in the stream emerging from space 50and the streams fed from hollow body 31 and its outlet ports 33;

The magnitude of the diverging angle of the secondary passageways 11;

The distance between the center of the secondary oxidant dischargeopenings 13 and the center of the fuel tube 45;

The number of discharge openings 13;

The velocity and the momentum of the streams exiting the secondarypassageways 11.

Lower NOx emission rates are expected for higher degree of staging. Thestaging limit is determined by the flame stability at the lowest NOx andCO emission rates of each set of combustion conditions. The presentinvention is capable of operating at firing densities within the rangefrom 60 to 500 kW/m³.

Advantages

The combustion method and apparatus disclosed herein allow fuel tocombust with oxidant streams presenting a total oxygen concentrationfrom the minimum required to promote flame stability up to 100%.

Another significant advantage is that the oxygen concentrations, and thefeed rates, of any or all of the oxidant streams can be changed whilecombustion continues, that is, without discontinuing and recommencingthe combustion.

In addition, the present invention produces satisfactorily low COemissions.

Other advantages of the present invention include the following:

The invention promotes the combustion process at any oxygenconcentration in oxidant within the range from 20.9 vol. % (or lower ifflame stability can be achieved) up to 100 vol. %, and have the oxygenconcentration changed during the ongoing combustion.

The invention promotes minimized NOx emission rate at each level ofoxygen concentration in the oxidant that is fed, with acceptable levelsof CO generation.

The invention minimizes NOx emission rates achieved at firing densitiescompatible with actual industrial furnaces, i.e., at firing densitieswithin the range from 60 to 500 kW/m³, with acceptable levels of COgeneration.

The invention avoids the need to provide two separate heating stations,one with oxygen-fired combustion and one with air-fired combustion, toaccommodate situations presenting different heat transfer rates.

Other advantages of the present invention appear in operationalapplications. For instance, yield improvement can be obtained inapplications where oxidation is a concern, such as aluminum melting andsteel reheating.

Specific fuel consumption is low, and is optimized, throughout thesequence of steps such as heating and holding operations.

Better and more uniform heat transfer and temperature distribution areattained.

Exemplary

In a metal melting process, a given target temperature (which can berelated to the charge temperature or to the product temperature or tothe furnace refractory temperature or to the flue gas temperature or acombination of them) can be achieved for different oxygen concentrationsin the oxidant streams fed to the burner system and combusted thereat.In order to achieve the best performance (in this case, rapid meltingrate), the application of pure oxygen is suitable for the melting phase.However, once the melting phase is completed, the use of pure oxygen incombusting the fuel is not economically justifiable. In accordance withthis invention, the total oxygen concentration in the oxidant streamsfed to the burner system and combusted thereat is reduced to a levelsufficient to keep the metal molten and hot.

Another example is that if the refractory lining of a ladle has to beheld at a given temperature for a long period of time, the burner systemcan be operated with the lowest total oxygen concentration that willsustain combustion at that given temperature. When there is a need toincrease the temperature of the ladle lining, the total oxygenconcentration is increased (on the fly) to the most economic (minimizedcost) level that raises the temperature at the desired rate. Improvedladle refractory heating and preheating, and extended refractorylifetime, are attained due to the ability to promote drying and curingwith a relatively low peak flame temperature (attained by carrying outcombustion with feeding of relatively low total oxygen concentration) innew refractory lining, and short heating cycle (higher heat transferrates, obtained by combusting with relatively higher total oxygenconcentration) in ladles in use to receive and hold molten metal.

Another example of the use of the method of the present invention is incontinuous or non-continuous steel reheat furnaces that are used to heatslabs of steel. For throughput increases, i.e., boosting, the presentinvention can be used by combusting fuel with oxidant streams having ahigh total oxygen concentration when the maximum throughput is required.If the throughput requirement lowers, then the total oxygenconcentration is lowered by an amount based on the new lower needs. Thatallows the burner system to be run at a steady rate (not going throughhigh fire and low fire modes) which would maintain steady furnacetemperature.

A simple quantitative example can be given in a ladle preheatingapplication. Preferred practice is to preheat a ladle, quickly, beforemolten metal is fed (“tapped”) into the ladle. The preheating increasesthe lifetime of the refractory (to avoid/minimize thermal shocks) and tominimize temperature drop of the molten metal tapped into the ladle. Forfast heating, combustion with a high total oxygen concentration is themost suitable application. If the ladle preheating station uses anoxy-air-burner that can only switch between oxy-fuel combustion (100%oxygen in the oxidant) and air-fuel combustion (combustion with air asthe only oxidant), the usual operation is to run the burner in oxy-fuelmode in the heating cycle to heat the ladle refractory lining quicklyand make the ladle available to the melt shop in a short period of time.When there is a delay in the melt shop the ladle is put “on hold” andthe burner would be operated with air (20.9% oxygen concentration inoxidant). If suddenly there is a requirement to heat up the ladlerefractory lining in such a way that the net energy required is of 1 MMBtu (293 kW) in 10 min, the burner could be switched to oxy-fuel modeand be operated intermittently, i.e., turned off when the set point isachieved and turned on when the temperature of the ladle refractorylining drops. This operation could cause thermal stress to the ladlerefractory lining lowering its useful life. Besides that, this type ofoperation could also cause problems (such as fatigue) to the valves onthe control system (because of the frequent repeated intermittent on/offoperation).

With the method of the present invention, the burner system could beoperated at the following condition. Assuming that the burner is ratedto fire 10 MM Btu/h (2930 kW), . . . if the net energy requirement is of1 MM Btu in 10 min and the burner is rated to deliver 1.7 MM Btu (500kW) in 10 min (10 MM Btu/h×10 min/60 min), this represents a thermalefficiency (or net heat available) of 60% throughout the 10 min ofoperation. Knowing the flue gas temperature would be 1200° C., theoxygen concentration in the total oxidant fed that corresponds to thenet heat available of 60% is determined to be 40% by volume. Thus, theburner described herein could be steadily operated by combusting fuelwith an oxidant stream containing 40% by volume of oxygen, which wouldpromote a smooth increase in temperature of the ladle refractory liningthereby avoiding unnecessary and undesired thermal stress.

If due to the production schedule requirement the heating rate needs tobe changed again, the same procedure would be put in practice, i.e., thetotal oxygen concentration in the oxidant streams fed to the burnersystem is varied on the fly, avoiding sudden changes in heat transfer.The fact that the total oxygen concentration can be varied whilecombustion is ongoing, without interrupting the combustion, andproviding any desired level of total oxygen concentration, brings aneconomic advantage since the combustion system can always be operated atthe minimum cost condition while promoting the lowest NOx emission atthat particular total oxygen concentration.

1. A method for heating a substrate, comprising: (A) providing a burnersystem comprising a burner body and a burner block, wherein (i) theburner body comprises a plenum body which has back and side surfacesthat enclose a plenum space which is open at its front in a uniplanarplenum opening that is defined by the front edges of said side surface,a feed inlet in a back or side surface of said plenum body, throughwhich gas can be fed into said plenum space, a first hollow body that issituated completely within said plenum space and that is closed againstpassage of gas between said plenum space and the interior of said hollowbody, wherein the hollow body does not extend through said plenumopening, a feed inlet through a surface of said hollow body, throughwhich gas can be fed into the interior of said hollow body, 2 to 16outlet ports through a surface of said hollow body, through which gascan pass out of said hollow body, each oriented to point outwardly ofsaid plenum space toward the plenum opening, wherein the outer ends ofsaid outlet ports do not extend beyond the plane of said plenum opening,a first tube extending from outside the back surface of said plenum bodythrough the plenum space to a first tube end that is located a firstdistance outside the plane of the plenum opening, wherein the first tubeis closed against passage of gas into said first tube from the plenumspace and from the interior of the hollow body, a second tube, locatedinside the first tube, extending from outside the back surface of saidplenum body through the plenum space to a second tube end that islocated a second distance outside the plane of the plenum opening,wherein said second distance is greater than first distance, whereinsaid second tube is closed against passage of gas into said second tubefrom the plenum space, from the interior of the hollow body, and fromthe first tube, and wherein the axes of the first and second tubes arecoaxial or parallel, a third tube, located inside the second tube,extending from outside the back surface of said plenum body through theplenum space to a third tube end that is located said second distanceoutside the plane of the plenum opening, wherein said third tube isclosed against passage of gas into said third tube from the plenumspace, from the interior of the hollow body, and from the second tube,and wherein the axes of the first, second and third tubes are coaxial orparallel, a feed inlet for receiving gas into the space between thefirst and second tubes, a feed inlet for receiving gas into the spacebetween the second and third tubes, and a feed inlet for receiving fuelinto said third tube; and (ii) the burner block comprises a frontsurface and a rear surface, a first passageway extending through theblock, composed of a barrel segment that extends into the block fromsaid rear surface to the inner end of said barrel segment for a lengthat least equal to said first distance, the diameter of said barrelsegment permitting said first tube to fit snugly into said barrelsegment to minimize passage of gas in said barrel segment outside saidfirst tube, a throat segment having upstream and downstream ends andwhose diameter is constant along its axis and is less than the diameterof said barrel segment and is greater than the outer diameter of saidsecond tube, wherein the distance from the rear surface of the block tosaid upstream end is greater than said first distance and less than saidsecond distance, and wherein the distance from the rear surface of saidblock to said downstream end is greater than said second distance, atapered segment that extends axially from the inner end of said barrelsegment to said upstream end of said throat segment, a port segment thatextends into the block from the front surface of the block to the innerend of the port segment, wherein the diameter of the port segment isconstant and is greater than the diameter of said throat segment a quarlsegment that extends from the downstream end of said throat segment tothe inner end of said port segment, wherein said segments are coaxial,and the sum of the axial lengths of the port segment and the quarlsegment is up to 50 times the diameter of the largest diameter of thequarl segment; the axial length of the throat segment is up to 50 timesthe diameter of the largest diameter of the quarl segment; the ratio ofthe largest diameter of the quarl segment to the diameter of the throatsegment is 1 to 50; and the distance from the discharge openings of thesecondary passageways to the axis of the first passageway is 1-10 timesthe diameter of the throat segment, a plurality of secondarypassageways, greater in number than the number of said outlet ports,extending through said block from inlet openings in the rear surface ofsaid block to discharge openings in the front surface of said block,wherein said inlet openings arc close enough to said first passagewaythat when the front edges of said plenum body are in contact with therear surface of said block, said inlet openings are in gas contact withsaid plenum space, and wherein each secondary passageway has an axis atits discharge opening that converges toward the axis of the firstpassageway at an angle of up to 60°, diverges from the axis of the firstpassageway at an angle of up to 85°, or is parallel to the axis of thefirst passageway; and wherein said burner body is positioned withrespect to said burner block so that the front edges of said plenum bodyare in contact with the rear surface of said block to prevent passage ofgas out of said plenum space except into said secondary passageways andthe first and second tubes extend into said first passageway, and outletports are aligned with secondary passageways so that gas passing from anoutlet port passes through a secondary passageway with which it isaligned. (B) determining a first rate of heat transfer to the substrate,(C) determining the rates at which fuel and oxidant are to be fed tosaid burner system to be combusted thereat, and the total oxygenconcentration of said oxidant to be combusted, to generate heat ofcombustion to be transferred to said substrate from said burner systemat said first rate, (D) feeding fuel, and oxidant having said totaloxygen concentration, at said rates to said burner system and combustingsaid fuel and said oxidant at said system to generate heat of combustionwhich is transferred to said substrate at said first rate, whileapportioning the amounts of oxygen fed through said first and secondtubes of said burner system with respect to the amounts of oxygen fedthrough said secondary passageways and said outlet ports of said burnersystem to minimize formation of NOx by said combustion, (E) determininga second rate of heat transfer to the substrate which is different fromsaid first rate, (F) determining a new total oxygen concentration ofsaid oxidant to be combusted and determining new rates at which saidoxidant, or said oxidant and said fuel, are to be fed to said burnersystem and combusted thereat to generate heat of combustion to betransferred to said substrate at said second rate, and (G) whilecontinuing to feed fuel and oxidant to said burner system, changing thetotal oxygen concentration fed to said burner system to said new totaloxygen concentration and changing the rate at which said oxidant or saidoxidant and said fuel are fed to said burner system, and continuing tocombust said fuel and oxidant at said burner system, withoutdiscontinuing said combustion, to generate heat of combustion which istransferred to said substrate at said second rate, while apportioningthe amounts of oxygen fed through said first and second tubes withrespect to the amounts of oxygen fed through said secondary passagewaysand said outlet ports to minimize formation of NOx by said combustion,wherein the amount of oxygen fed to said burner system is at all timessufficient to maintain combustion of said fuel at said burner system,and wherein the amount of oxygen fed to said burner system is at alltimes sufficient to maintain the carbon monoxide content of the gaseousproducts of said combustion at less than 100 ppm.
 2. (canceled)
 3. Amethod according to claim 1 wherein heat is transferred to saidsubstrate at said first rate to melt all or a portion of said substrate,and heat is transferred to said substrate at said second rate tomaintain said molten substrate in the molten state.
 4. A methodaccording to claim 1 wherein said substrate is a ladle, heat istransferred to said ladle at a first rate to heat the ladle, and heat istransferred to said ladle at said second rate to a higher temperature.5. A method according to claim 1 wherein heat is transferred at saidfirst rate in a steel reheating furnace to slabs of steel passingthrough said furnace at a first rate of throughput, and heat istransferred at said second rate to slabs of steel passing through saidfurnace a second rate of through put different from said first rate ofthroughput.